CN102372567A - Method for producing ethene by ethanol dehydration - Google Patents
Method for producing ethene by ethanol dehydration Download PDFInfo
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- CN102372567A CN102372567A CN2010102608066A CN201010260806A CN102372567A CN 102372567 A CN102372567 A CN 102372567A CN 2010102608066 A CN2010102608066 A CN 2010102608066A CN 201010260806 A CN201010260806 A CN 201010260806A CN 102372567 A CN102372567 A CN 102372567A
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Abstract
The invention relates to a method for producing ethene by ethanol dehydration and mainly solves the problem of high device energy consumption and high material consumption during the process flow of producing ethene by ethanol dehydration in the prior art. The method for producing ethene by ethanol dehydration in the invention comprises the following steps of: allowing 5-99.99wt% of an ethanol raw material at 25-100 DEG C to enter into the top of a stripping tower, allowing 1-10wt% of recovered ethanol to enter into the central portion of the stripping tower, carrying out pervaporation separation in the stripping tower, allowing pure ethanol steam obtained on the top of the stripping tower to enter into an ethanol dehydration reaction system, and continuously discharging tower bottom liquids of the stripping tower bottom out of the system. The technical scheme greatly solves the problem and can be used in the industrial production of ethene by ethanol dehydration.
Description
Technical field
The present invention relates to a kind of method that is used for the technology of producing ethylene from dehydration of ethanol.
Background technology
Ethene is crucial petrochemical materials, and its large derived product mainly contains Vilaterm, oxyethane, terepthaloyl moietie, SE, vinylbenzene, vinyl acetate between to for plastic etc.
Production technique (the Gu Zhihua of existing ethylene prepared by catalytic dehydration of ethylene; The producing ethylene with ethyl alcohol state of the art and prospect [J]. chemical progress; 2006; 25 (8): production process 847-851) is: feed ethanol through preheater, vaporizer heating back all vaporization send the ethanol dehydration reaction system to react, after the reaction product (containing resultant of reaction ethene, water, unreacted ethanol etc.) of coming out from the dehydration reaction system is sent washing, scale to wash etc. to wash removal impurity; After compression, drying, get into ethylene rectification tower and carry out rectifying separation, obtain ethylene product from ethylene rectification tower top or cat head; And the ethanol of discharging from the tower still is sent to waste-water treatment tower with the mixed solution of components such as water together with the water wash column tower bottoms.
One of characteristics of existing method are that special waste-water treatment tower need be set; With with the method for rectifying with the ethanol separation removal in the mixed solution of components such as the ethanol of water wash column and ethylene distillation Tata still and water, moisture (these moisture derive from the water that the water that adds in the water washing process, moisture that feed ethanol is brought and dehydration reaction produce) is then discharged system from wastewater treatment Tata still.Because will add a large amount of water in the water washing process again, so the treatment capacity of general waste-water treatment tower is bigger, and; Ethanol obtains from wastewater treatment column overhead (evaporation back condensation); And need certain reflux ratio, and therefore need to consume a large amount of heat energy, cause the energy consumption of device high.
Two of the characteristics of existing method are the ethanol as raw material; No matter water cut is how much, all vaporizations in vaporizer, the also just whole vaporization entering gas-phase dehydration of moisture wherein reactive system; Increase the required heat energy of water vapor so greatly, caused the energy consumption of device high.
Be not provided for reclaiming the alcoholic acid treating column in the existing procedure simultaneously, and the still liquid of directly ethylene distillation Tata still being drawn is discharged into out-of-bounds as waste water with the water wash column tower bottoms, causes alcoholic acid to lose in a large number, causes the material consumption of device very big.
Summary of the invention
Technical problem to be solved by this invention is plant energy consumption and the high problem of material consumption in the technological process of production of existing producing ethylene from dehydration of ethanol, and a kind of method of new producing ethylene from dehydration of ethanol is provided.It is little that this method has the ethanol loss, device material consumption and advantage of low energy consumption.
In order to solve the problems of the technologies described above; The technical scheme that the present invention adopts is following: a kind of method that is used for producing ethylene by ethanol dehydration, temperature are 25～100 ℃, and weight content is 5～99.99% ethanol raw material entering gas stripping column top; Weight content is 1～10% recovery ethanol entering gas stripping column middle part; Realize that in gas stripping column vaporization separates, obtain straight alcohol steam from the gas stripping column cat head and get into the ethanol dehydration reaction system that the still liquid of gas stripping column tower still is discharged system continuously.
In the technique scheme, optimized technical scheme is that the temperature of the feed ethanol on entering gas stripping column top is 25～50 ℃.Gas stripping column is packing tower or tray column, and its theoretical plate number is 10～50, and wherein rectifying section is 5～50 blocks of theoretical trays, and tower top pressure is 0.6～4.0MPaG, and tower top temperature is-15～-50 ℃.The upper and lower of gas stripping column middle part opening for feed all is provided with the tower joint with separating power, and ethanol content is 0.01～0.2Wt% in the gas stripping column tower still liquid effluent.
As stated; The present invention adopts the gas stripping column that has the ethanol dual-use function in vaporization feed ethanol and Separation and Recovery water wash column tower bottoms and the ethylene distillation Tata still mixed solution concurrently; Not only save the investment of waste-water treatment tower and support equipment thereof; The alcoholic acid energy consumption of removing in the mixed solution is reduced significantly, reclaimed simultaneously and do not sent out the ethanol of answering, further reduced the material consumption of device.
Because gas stripping column need be with cat head alcohol vapour condensing reflux; And the alcoholic acid purity of cat head vaporization generally speaking is higher than the purity of feed ethanol, the required heat energy of ethanol so the required heat energy of ethanol in gas stripping column Separation and Recovery washing Tata still and ethylene distillation Tata still mixed solution is just vaporized.Obviously, the present invention comes the alcoholic acid energy consumption in Separation and Recovery washing Tata still and the ethylene distillation Tata still mixed solution with gas stripping column, compares with the existing method that is provided with waste-water treatment tower, and energy consumption reduces significantly.
Gas stripping column of the present invention is with water vapour and the direct Hybrid Heating of tower bottoms body, and the investment that both can save reboiler can reduce the consumption of water vapour again.Because water vapour directly mixes with the tower bottoms body; The condensing temperature that adds the hot steam equals tower still temperature; The heat utilization efficiency of water vapour high (condensing temperature of water vapour is low more, and the condensation latent heat of water vapour is big more, and the sensible heat of water vapour also all has been utilized); So reduced the consumption of water vapour, reduced the energy consumption of device.
The present invention be advantageous in that; No matter purity of alcohol how in the feed ethanol; Because vaporization purification tower structure is unique, vaporization purification tower bottoms is discharged continuously; Purity of alcohol from the steam that vaporization purification tower cat head obtains always than the purity of alcohol of feed ethanol slightly high (be in the raw material moisture have only the part vaporization), has significantly reduced feed vaporization institute energy requirement generally speaking, has reduced the energy consumption of installing.
Among the present invention; Owing to adopt the unique technology and the structure of ethanol gas stripper; And with the ingenious combination of water wash column and ethylene rectification tower; Be used for realizing separating purifying reclaiming the ethanol of washing Tata still and ethylene distillation Tata still mixed solution, can significantly reduce the energy consumption and the material consumption of device, obtained the better economic effect.
Description of drawings
Fig. 1 is the technical process of producing ethylene from dehydration of ethanol of the present invention.
Among Fig. 1,1 is feed ethanol, and 2 is the ethanol preheater, and 3 are the ethanol after the preheating; 4 mixed solutions for recovery, 5 is gas stripping column, and 6 is alcohol vapour, and 7 is the discharging of gas stripping column tower still; 8 are gas or low pressure water vapor after boiling again, and 9 is the gas stripping column reboiler, 10 gas stripping column tower bottomss.
Purity is the at first preheating in ethanol preheater 2 of ethanol raw material 1 of 5～100 volume %; Ethanol 3 after the preheating gets into gas stripping column 5 from cat head; Reclaim with water and ethanol be the mixed solution 4 of major ingredient from the middle part entering gas stripping column 5; All after vaporization separated, the alcohol vapour 6 that gas stripping column 5 cats head obtain got into follow-up system to ethanol in these two bursts of chargings.Gas stripping column 5 tower stills perhaps with reboiler 9 heating stripper tower still dischargings 7, are perhaps directly used water vapour 8 direct and tower still discharging 7 Hybrid Heating, and gas stripping column 5 tower still still liquid 10 send Waste Water Treatment.
Through embodiment the present invention is done further elaboration below.
Embodiment
[embodiment 1]
Adopt technical process shown in Figure 1, gas stripping column is a tray column, and theoretical plate number is 50, working pressure 0.6MPa (G).Feed ethanol 2350kg/h, ethanol 1997.5kg/h wherein, water 352.5kg/h, ethanol content 85% (wt%).Feed ethanol is from the charging of gas stripping column cat head.Ethanol 66.08kg/h in the mixed solution that reclaims, water 1932kg/h, feed entrance point is at gas stripping column cat head number the 8th theoretical stage place.Gas stripping column cat head exhaust vapour send the dehydration reaction system, wherein ethanol content 93.8% (wt%).Ethanol contains 0.05% (wt%) in the water that gas stripping column tower still is discharged.
[embodiment 2]
Adopt technical process shown in Figure 1, gas stripping column is a tray column, and theoretical plate number is 30, operation table pressure pressure 0.9MPaG.Feed ethanol 2350kg/h, ethanol 2210kg/h wherein, water 140kg/h, ethanol content 94% (wt%).Feed ethanol is from the charging of gas stripping column cat head.Ethanol 76.25kg/h in the mixed solution that reclaims, water 1725kg/h, feed entrance point is at gas stripping column cat head number the 21st theoretical stage place.The gas stripping column cat head is discharged alcohol vapour and is sent the dehydration reaction system, wherein ethanol content 98% (wt%).Ethanol content 0.1% (wt%) in the water that gas stripping column tower still is discharged.
[embodiment 3]
Adopt technical process shown in Figure 1, gas stripping column is a tray column, and theoretical plate number is 10, operation table pressure pressure 4MPaG.Feed ethanol 2350kg/h, ethanol 1739kg/h wherein, water 611kg/h, ethanol content 74% (wt%).Feed ethanol is from the charging of gas stripping column cat head.Ethanol 46.25kg/h in the mixed solution that reclaims, water 1725kg/h, feed entrance point is at gas stripping column cat head number the 21st theoretical stage place.The gas stripping column cat head is discharged alcohol vapour and is sent the dehydration reaction system, wherein ethanol content 90% (wt%).Ethanol content 0.08% (wt%) in the water that gas stripping column tower still is discharged.
[embodiment 4]
Adopt technical process shown in Figure 1, gas stripping column is a packing tower, operation table pressure pressure 0.5MPaG.Feed ethanol 2350kg/h, ethanol 2210kg/h wherein, water 140kg/h, ethanol content 94% (wt%).Feed ethanol is from the charging of gas stripping column cat head.Ethanol 66.25kg/h in the mixed solution that reclaims, water 1725kg/h, feed entrance point is at gas stripping column cat head number the 11st theoretical stage place.The gas stripping column cat head is discharged alcohol vapour and is sent the dehydration reaction system, wherein ethanol content 95% (wt%).Ethanol content 0.06% (wt%) in the water that gas stripping column tower still is discharged.
[comparative example 1]
Adopt feed ethanol directly through the scheme of ethanol evaporation device evaporation back entering reactive system, feed ethanol 2350kg/h, ethanol 2210kg/h wherein, water 140kg/h, ethanol content 94% (wt%).Ethanol content 0.5% (wt%) in the waste water that tower bottoms is discharged.
Claims (5)
1. method that is used for producing ethylene by ethanol dehydration; Temperature is 25～100 ℃; Weight content is 5～99.99% ethanol raw material entering gas stripping column top, and weight content is 1～10% recovery ethanol entering gas stripping column middle part, in gas stripping column, realizes the vaporization separation; Obtain straight alcohol steam from the gas stripping column cat head and get into the ethanol dehydration reaction system, the still liquid of gas stripping column tower still is discharged system continuously.
2. according to the said a kind of method that is used for producing ethylene by ethanol dehydration of claim 1, the temperature that it is characterized in that getting into the feed ethanol on gas stripping column top is 25～50 ℃.
3. according to the said a kind of method that is used for producing ethylene by ethanol dehydration of claim 1; It is characterized in that gas stripping column is packing tower or tray column, its theoretical plate number is 10～50, and wherein rectifying section is 5～50 blocks of theoretical trays; Tower top pressure is 0.6～4.0MPaG, and tower top temperature is-15～-50 ℃.
4. according to the said a kind of method that is used for producing ethylene by ethanol dehydration of claim 1, it is characterized in that the upper and lower of the middle part opening for feed of gas stripping column all is provided with the tower joint with separating power.
5. according to the said a kind of method that is used for producing ethylene by ethanol dehydration of claim 1, it is characterized in that ethanol content is 0.01～0.2Wt% in the tower still liquid effluent.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242136A (en) * | 2013-04-28 | 2013-08-14 | 江门谦信化工发展有限公司 | Method for recycling alcohol from butyl acrylate wastewater |
| CN103539604A (en) * | 2012-07-12 | 2014-01-29 | 中国石油化工股份有限公司 | Production method for preparing ethylene through ethanol dehydration |
| CN103539214A (en) * | 2012-07-12 | 2014-01-29 | 中国石油化工股份有限公司 | Method for treating organic wastewater generated in preparing ethylene through ethanol dehydration |
| CN104230623A (en) * | 2013-06-17 | 2014-12-24 | 中国石油化工股份有限公司 | Energy-efficient method for ethylene production from ethanol dehydration |
| CN104276918A (en) * | 2013-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Organic wastewater treatment method of ethanol dehydration for preparation of ethene |
| CN104447167A (en) * | 2014-12-11 | 2015-03-25 | 西南化工研究设计院有限公司 | New process for preparing high-purity isobutene from tertiary butanol |
| US9738575B2 (en) | 2012-05-16 | 2017-08-22 | China Petroleum & Chemical Corporation | Apparatus for producing ethylene and a producing method thereof |
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| CN101801488A (en) * | 2007-07-13 | 2010-08-11 | Amt国际股份有限公司 | Low-energy extractive distillation process for dehydration of aqueous ethanol |
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| CN101801488A (en) * | 2007-07-13 | 2010-08-11 | Amt国际股份有限公司 | Low-energy extractive distillation process for dehydration of aqueous ethanol |
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| 顾志华: "乙醇制乙烯技术现状及展望", 《化工进展》 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9738575B2 (en) | 2012-05-16 | 2017-08-22 | China Petroleum & Chemical Corporation | Apparatus for producing ethylene and a producing method thereof |
| CN103539604A (en) * | 2012-07-12 | 2014-01-29 | 中国石油化工股份有限公司 | Production method for preparing ethylene through ethanol dehydration |
| CN103539214A (en) * | 2012-07-12 | 2014-01-29 | 中国石油化工股份有限公司 | Method for treating organic wastewater generated in preparing ethylene through ethanol dehydration |
| CN103539604B (en) * | 2012-07-12 | 2015-06-10 | 中国石油化工股份有限公司 | Production method for preparing ethylene through ethanol dehydration |
| CN103242136A (en) * | 2013-04-28 | 2013-08-14 | 江门谦信化工发展有限公司 | Method for recycling alcohol from butyl acrylate wastewater |
| CN104230623A (en) * | 2013-06-17 | 2014-12-24 | 中国石油化工股份有限公司 | Energy-efficient method for ethylene production from ethanol dehydration |
| CN104230623B (en) * | 2013-06-17 | 2016-08-17 | 中国石油化工股份有限公司 | The energy-saving production method of producing ethylene from dehydration of ethanol |
| CN104276918A (en) * | 2013-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Organic wastewater treatment method of ethanol dehydration for preparation of ethene |
| CN104447167A (en) * | 2014-12-11 | 2015-03-25 | 西南化工研究设计院有限公司 | New process for preparing high-purity isobutene from tertiary butanol |
| CN104447167B (en) * | 2014-12-11 | 2016-02-10 | 西南化工研究设计院有限公司 | High-purity iso-butylene novel process is prepared by the trimethyl carbinol |
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